A method for catalytic vapor phase oxidation of methanol to formaldehyde may include: passing a feed stream comprising methanol and oxygen through a layered catalyst bed having a first layer comprising a first silver catalyst particles and a second layer comprising a second silver catalyst particles that are different than the first silver catalyst particles, wherein the feed stream passes through the first layer before the second layer, wherein the first silver catalyst particles has a greater reaction activity for converting methanol and oxygen to formaldehyde; and reacting the methanol and the oxygen in the presence of the catalysts to produce a product stream comprising formaldehyde.

Systems and processes disclosed may be used to produce a high purity isobutane stream and a high purity 1-butene stream from mixed C4 streams having disparate starting compositions.

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different.

Reactor systems, reactor coolant systems, and associated processes for polymerizing polyolefins are described. The reactor systems generally include a reactor pipe and a coolant system, in which the coolant system includes a jacket pipe surrounding at least a portion of the reactor pipe to form an annulus therebetween, at least one spacer coupling the jacket to the reactor pipe, and a coolant which flows through the annulus to remove heat from the reactor pipe. At least one of the external surface of the reactor pipe, the internal surface of the jacket, and at least one spacer, are independently modified, for example by polishing, coating, or reshaping, to reduce the fluid resistance of the coolant flow through the annulus.

Methods of simultaneously converting butanes and methanol to olefins over Ti-containing zeolite catalysts are described. The exothermicity of the alcohols to olefins reaction is matched by endothermicity of dehydrogenation reaction of butane(s) to light olefins resulting in a thermo-neutral process. The Ti-containing zeolites provide excellent selectivity to light olefins as well as exceptionally high hydrothermal stability. The coupled reaction may advantageously be conducted in a staged reactor with methanol/DME conversion zones alternating with zones for butane(s) dehydrogenation. The resulting light olefins can then be reacted with iso-butane to produce high-octane alkylate. The net result is a highly efficient and low cost method for converting methanol and butanes to alkylate.

Methods of simultaneously converting butanes and methanol to olefins over Ti-containing zeolite catalysts are described. The exothermicity of the alcohols to olefins reaction is matched by endothermicity of dehydrogenation reaction of butane(s) to light olefins resulting in a thermo-neutral process. The Ti-containing zeolites provide excellent selectivity to light olefins as well as exceptionally high hydrothermal stability. The coupled reaction may advantageously be conducted in a staged reactor with methanol/DME conversion zones alternating with zones for butane(s) dehydrogenation. The resulting light olefins can then be reacted with iso-butane to produce high-octane alkylate. The net result is a highly efficient and low cost method for converting methanol and butanes to alkylate.

A process for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 % wt. to 0.5 % wt.. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil. A device for conducting the process is also disclosed.

The invention relates to a process, unit and reaction system of low-carbon alkane dehydrogenation, which comprises the following steps: C3-C5 low-carbon alkane feed gas, together with CO and/or CO.sub.2 process gas, get into reactor after being preheated to 200-500° C., contact with a Cr—Ce—Cl/Al.sub.2O.sub.3 dehydrogenation catalyst, a Cu—Ce—Ca—Cl/Al.sub.2O.sub.3 thermal generating agent and thermal storage/support inert alumina balls, and convert to dehydrogenation products for 5-30 minutes under the conditions: temperature, 500-700° C., pressure, 10-100 kPa and weight hourly space velocity (WHSV), 0.1-5 hours.sup.−1. The products formed enter the downstream separation unit for separating out the low-carbon alkenes. The periodic regeneration process of the catalyst bed includes steam purging, hot air regenerating, bed heating, evacuating and reducing at 560 to 730° C. and 0.01 to 1 MPa. Each cycle needs about 10-70 minutes. With such dehydrogenation process, the reaction heat balance is moderated, and temperature gradient and reaction severity in the catalyst bed are reduced. As a consequence, the catalytic conversion, product selectivity, operation cycle and service life are improved. The system energy consumption is reduced.

A system for methanol synthesis from a synthesis gas rich in hydrogen and CO2/CO having a first adiabatic reactor (11) with a structure having an inlet stream (10), a first catalytic bed (12), one Venturi type mixing element (13), a first divergent nozzle (14), a second catalytic bed (27) and one outlet stream (28) all of them connected sequentially to each other; a first heat exchanger (15) connected to the outlet stream (28) downstream the reactor (11); a condenser (16) connected to the heat exchanger (15) downstream of the heat exchanger (15); a separator (18) connected to the condenser (16); a first cold gas stream (19) joining the separator (18) to both the first heat exchanger (15) and the first Venturi type mixing element (13); a first outlet stream (21) joining the heat exchanger (15) to a second adiabatic reactor (24) similar to the first adiabatic reactor (11).

A system for methanol synthesis from a synthesis gas rich in hydrogen and CO2/CO having a first adiabatic reactor (11) with a structure having an inlet stream (10), a first catalytic bed (12), one Venturi type mixing element (13), a first divergent nozzle (14), a second catalytic bed (27) and one outlet stream (28) all of them connected sequentially to each other; a first heat exchanger (15) connected to the outlet stream (28) downstream the reactor (11); a condenser (16) connected to the heat exchanger (15) downstream of the heat exchanger (15); a separator (18) connected to the condenser (16); a first cold gas stream (19) joining the separator (18) to both the first heat exchanger (15) and the first Venturi type mixing element (13); a first outlet stream (21) joining the heat exchanger (15) to a second adiabatic reactor (24) similar to the first adiabatic reactor (11).